EP1342694A1 - Procédé et dispositif pour le réformage d'hydrocarbures contenus dans un gaz d'alimentation - Google Patents

Procédé et dispositif pour le réformage d'hydrocarbures contenus dans un gaz d'alimentation Download PDF

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Publication number
EP1342694A1
EP1342694A1 EP03090050A EP03090050A EP1342694A1 EP 1342694 A1 EP1342694 A1 EP 1342694A1 EP 03090050 A EP03090050 A EP 03090050A EP 03090050 A EP03090050 A EP 03090050A EP 1342694 A1 EP1342694 A1 EP 1342694A1
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EP
European Patent Office
Prior art keywords
reforming
feed gas
reforming section
section
gas
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP03090050A
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German (de)
English (en)
Inventor
Dieter Schlegel
Robert Szolak
Ulrich Hofmann
Marc Straub
William Wiesner
Bernd Tischhauser
Markus Löhr
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Mahler AGS GmbH
Fraunhofer Gesellschaft zur Forderung der Angewandten Forschung eV
Original Assignee
Mahler AGS GmbH
Fraunhofer Gesellschaft zur Forderung der Angewandten Forschung eV
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Publication date
Application filed by Mahler AGS GmbH, Fraunhofer Gesellschaft zur Forderung der Angewandten Forschung eV filed Critical Mahler AGS GmbH
Publication of EP1342694A1 publication Critical patent/EP1342694A1/fr
Withdrawn legal-status Critical Current

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0496—Heating or cooling the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
    • B01J8/0461—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds
    • B01J8/0465—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds the beds being concentric
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/384—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts the catalyst being continuously externally heated
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
    • B01J2208/00132—Tubes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00309—Controlling the temperature by indirect heat exchange with two or more reactions in heat exchange with each other, such as an endothermic reaction in heat exchange with an exothermic reaction
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00504—Controlling the temperature by means of a burner
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/0053—Controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • C01B2203/0816—Heating by flames
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1005—Arrangement or shape of catalyst
    • C01B2203/1011—Packed bed of catalytic structures, e.g. particles, packing elements
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1241—Natural gas or methane
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/14—Details of the flowsheet
    • C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
    • C01B2203/82—Several process steps of C01B2203/02 - C01B2203/08 integrated into a single apparatus

Definitions

  • the present invention relates to a device and a method for reforming hydrocarbons from a feed gas according to claims 1 and 17, respectively.
  • WO 98/528 68 A1 shows a generic object.
  • a device for reforming hydrocarbons from a feed gas with a reforming reactor and a flue gas Burner shown for heating the reforming reactor contains a radiant burner which is arranged around two radially layered reforming sections.
  • a feed gas which contains, for example, steam and natural gas, is fed to the inner reforming section.
  • heat is convectively supplied by the radiant burner or flue gas originating from this radiant burner.
  • the feed gas is partially reformed in the first reforming section by catalyst material applied to metal honeycombs.
  • the partially reformed feed gas is then fed to the reforming section, which surrounds the first reforming section in a ring, and which likewise has metal honeycombs covered with catalyst material. Heat is applied to this second, outer reforming section by the burner by convection and by radiation. After passing through the second reforming section, the hydrocarbons contained there are almost completely converted.
  • the device for reforming shown there is in principle functional, but in practice the radiation burner proposed there (which has ceramic perforated plates) has the disadvantages of complicated controllability, sensitivity of the ceramic plates and high overall costs for larger firing capacities. In addition, the metal honeycombs contained there are also quite expensive and their structure must always be designed for the special system.
  • the object of the present invention is an apparatus and a method for reforming To make available, which is particularly suitable for the production of small and medium amounts of hydrogen, and is inexpensive to manufacture and still allows a good efficiency or a quick start and stop.
  • a particularly advantageous development of the device provides that the outer reforming section for the passage of the feed gas is connected upstream of the inner reforming section and the pipes running in the direction of the longitudinal axis run through the outer reforming section.
  • this enables a process temperature which is relatively homogeneous in all reforming sections.
  • the inner reforming section is heated convectively and by radiation from the burner, the outer reforming section is additionally heated homogeneously by the pipes arranged therein.
  • both the outer and the inner reforming section each have an annular cross section or an annular cylindrical shape. It is advisable that the tubes are distributed over the circumference of the outer reforming section in order to achieve particularly homogeneous heat spreading in the outer reforming section.
  • these tubes alternately carry different hot gases distributed over the circumference of the reforming section, e.g. Lead a pipe of flue gas and an adjacent pipe of partially or fully reformed feed gas in a periodic sequence.
  • the reforming sections each have an essentially annular-gap-shaped cross-section, with the burner arranged in the innermost section, which preferably has a cylindrical radiation tube in the longitudinal direction for heat homogenization or flue gas conduction and a further annular gap between the layered reforming sections for guiding partially reformed ones Feed gas is provided.
  • the feed gas for initial heating can be conducted, for example, in counterflow with flue gas or reformed and thus heated feed gas
  • a particularly advantageous embodiment provides that the reforming sections with an annular gap-shaped cross section in the radial direction have gap sizes smaller than 50 mm, preferably smaller than 25 mm exhibit. These small gap widths make it possible to ensure even smaller temperature gradients in the radial direction across the annulus.
  • the reforming sections themselves can be filled in different ways. On the one hand, it is possible to use a gas-conducting metal honeycomb structure NiO catalyst material is coated, to ensure good implementation of the feed gas.
  • spherical support materials made of calcium aluminate or aluminum oxide are provided within the reforming sections with catalyst material. These are e.g. coated with NiO reforming catalyst in the wash coat process.
  • the efficiency of this filling of the reforming reactor hardly lags behind that of good metal honeycomb structures, but the material costs are significantly lower and, above all, filling the reforming sections is particularly easy to ensure, this also applies to the complete exchange of used material.
  • the spherical carrier materials have a diameter between 3 and 6 mm, preferably between 4 and 5 mm.
  • An advantageous embodiment of the method according to the invention provides that the conversion of the hydrocarbons contained in the feed gas is 30-50% in each reforming section. Depending on the design of the reforming reactor the distribution of the proportional implementation in the individual reform sections can be controlled. Overall, it is even possible to ensure a total conversion of the hydrocarbons contained in the feed gas of over 97% with a relatively low manufacturing cost using the method and the device according to the invention.
  • the total conversion X c is defined here as the difference between the molar amount of carbon atoms C in hydrocarbons C N H M contained in the feed gas and the molar amount of (methane) CH 4 contained in the reformate based on the molar amount of C atoms in hydrocarbons contained in the feed gas :
  • the pressure in the reforming sections is between 0 and 1.75 bar.
  • the exit temperature of the reformed feed gas after leaving the second reforming section is between 680 and 740 degrees Celsius, preferably between 700 and 730 degrees Celsius.
  • the material loads can be significantly reduced.
  • the temperature of the radiant tube surrounding the burner can also be reduced in comparison with conventional designs, with the same radiant power of the burner. This means that commercially available stainless steel can be used, which is cheaper to buy and process than ceramics required at higher temperatures.
  • Figures 1 and 2 show two orthogonal sections through a device according to the invention.
  • This is a device 1 for reforming hydrocarbons from a feed gas 2 with a reforming reactor 3 and a burner 4 emitting flue gas for heating the reforming reactor, the reforming reactor having two reforming sections 3a and 3b, in which the one reforming section 3a along a longitudinal axis 5 is arranged around the other reforming section 3b.
  • the key here is that within the Catalytically active region of the reforming section 3a, through which feed gas flows, tubes 6a, 6b extending in the direction of the longitudinal axis 5 are arranged for the passage of hot gases.
  • the device 1 is arranged essentially rotationally symmetrically with respect to the longitudinal axis 5.
  • a feed gas flows into the device through an upper inlet 13.
  • This feed gas 2 contains a mixture of, for example, natural gas, biogas or landfill gas and steam.
  • the gas flows circumferentially radially outward through a radial channel 14.
  • the feed gas 2 is heated in countercurrent by product gas / reformate 8 (ie practically completely reformed feed gas).
  • the heated feed gas 2 flows into a ring-shaped first reforming section 3a. In this reforming section, the thickness of the catalyst layer between two heated walls is less than 25 mm.
  • the annular gap-shaped reforming section 3a extends along the longitudinal axis 5 as the central axis and has a plurality of tubes 6a and 6b distributed over its circumference in the inner annular gap, approximately in the central radial region.
  • the annular gap of the reforming section 3a is filled with a bed 15.
  • This bed consists of balls with a diameter of 4-5mm.
  • the balls consist of a spherical carrier material made of calcium aluminate. This carrier material is coated with NiO reforming catalyst using the wash-coat process.
  • the tubes 6a and 6b run in the radial direction approximately in the middle of this layering, so that the layering essentially completely surrounds the tubes 6a and 6b.
  • the tubes 6a and 6b are accommodated alternately distributed over the circumference in the bed of the reforming section 3a.
  • the small diameter tubes are designated 6a, the large diameter tubes 6b.
  • the tubes 6a carry essentially completely reformed feed gas (reformate) 8 in countercurrent with respect to the flow of the feed gas 2 in the bed, the tubes 6b lead flue gas originating from the burner 4 essentially in counterflow to the feed gas 2 inside the bed.
  • the tubes 6a and & b alternate, through these tubes a "temperature bridge" is formed from the outer to the inner circumference of the annular gap, so that a homogeneous temperature distribution with a results in low temperature gradients.
  • the feed gas 2 After the feed gas 2 has passed through the bed (directed vertically downwards in FIG. 1), it is passed through a radial deflection 16 and then guided vertically upwards in an annular gap 9 in the longitudinal direction 5.
  • a radial deflection 16 When passing through the radial deflection 16, 30 to 50% of the hydrocarbons contained in the feed gas are converted to hydrogen.
  • the annular gap 9 has on its outer circumference a stainless steel wall, which contains the bed of the reforming section 3a on its radially outer side.
  • a thermally insulating layer 17 is attached to the radial inner wall of the annular gap 9.
  • a second inner reforming section 3b is arranged radially within this insulating wall 17. This is in the form of an annular gap the longitudinal axis 5 is formed around and arranged concentrically to the reforming section 3a.
  • the reforming section 3b is filled with the same fill as the reforming section 3a and has essentially the same height.
  • the partially reformed feed gas 10 After the partially reformed feed gas 10 has passed through the annular gap 9 upwards, it passes a further radial deflection 24 and is guided radially inwards there and then again vertically downwards in direction 5 through the bed of the reforming section 3b. When this bed is passed again 30-50% of the (based on the feed gas 2 introduced through the upper inlet 13) of the hydrocarbons are converted.
  • the now reformed feed gas 8 passes radially outwards through a further radial deflection 18 and is guided upwards from there through the pipes 6a in direction 5, as shown in FIG. 1, where it follows vertically after two further radial deflections 19 and 20 is led away above and in the countercurrent first heated the feed gas 2 in the reforming section 3b and then the feed gas flowing through the radial channel 14 or the upper inlet 13.
  • All of the channels described above can be made from relatively inexpensive stainless steel materials.
  • the thickness of the sheets installed there is preferably between 2 and 7 mm. This is possible because the temperatures in the reforming reactor are relatively low, so the reformed feed gas 8 has a temperature between 680 and 740 degrees Celsius, preferably between 700 and 730 degrees Celsius, when the second reforming section 3b emerges.
  • the flow resistance of the reforming sections, which are filled with a bed, is relatively low, so that a pressure between 0 and 1.75 bar in the reforming reactor is sufficient to pass the feed gas.
  • steam reforming works here with particularly high degrees of conversion X c .
  • the entire arrangement is heated via a burner 4 arranged in the center of the device.
  • the burner is radially surrounded by a radiation tube 12 which rests on the underside of the device 1.
  • a combustible gas is burned to form flue gas with the release of thermal energy.
  • the flue gas is first guided vertically upwards in direction 5 and there is directed through a radial deflection 21 to the side of the radiation tube 12 facing away from the burner 4.
  • the flue gas 7 is guided vertically downward in an annular gap 22 and there, orthogonally, guided laterally outward radially by a radial deflection 23.
  • the inner reforming section 3b is heated from the inside by the radiation from the radiation tube 12 and by convective heat transfer of the flue gas 7.
  • the flue gas 7 After passing through the radial deflection 23, the flue gas 7 is then guided vertically upwards through pipes 6b, whereby it heats the feed gas 2 passed through the bed of the reforming section 3a in countercurrent and thus contributes to the catalytic conversion of the hydrocarbons contained in the feed gas 2.
  • burners that emit flue gas are preferably used as burners, since their hot exhaust gases can be used thermally here in a particularly useful manner.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Hydrogen, Water And Hydrids (AREA)
EP03090050A 2002-03-04 2003-03-04 Procédé et dispositif pour le réformage d'hydrocarbures contenus dans un gaz d'alimentation Withdrawn EP1342694A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE2002109886 DE10209886A1 (de) 2002-03-04 2002-03-04 Vorrichtung sowie Verfahren zur Reformierung von Kohlenwasserstoffen aus einem Einsatzgas
DE10209886 2002-03-04

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EP1342694A1 true EP1342694A1 (fr) 2003-09-10

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EP (1) EP1342694A1 (fr)
DE (1) DE10209886A1 (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006045746A1 (fr) * 2004-10-20 2006-05-04 Shell Internationale Research Maatschappij B.V. Procede de preparation d'un melange de monoxyde de carbone et d'hydrogene
WO2006045744A1 (fr) * 2004-10-20 2006-05-04 Shell Internationale Research Maatschappij B.V. Procede pour le reformage de vapeur et/ou de co2 d'une matiere premiere hydrocarbonee
EP2495214A3 (fr) * 2011-03-04 2013-01-23 DBI- Gastechnologisches Institut gGmbH Freiberg Procédé et dispositif pour reformage vapeur de gaz contenant des hydrocarbures
CN105189345A (zh) * 2013-03-25 2015-12-23 住友精密工业株式会社 燃料改性器及燃料电池
WO2020035706A1 (fr) * 2018-08-17 2020-02-20 Geoffrey Gerald Weedon Reformage à la vapeur ou à sec d'hydrocarbures

Citations (4)

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Publication number Priority date Publication date Assignee Title
WO1988001983A2 (fr) * 1986-09-15 1988-03-24 L. & C. Steinmüller Gmbh Reformeur pour le craquage catalytique d'hydrocarbures gazeux
EP0360505A2 (fr) * 1988-09-19 1990-03-28 Kabushiki Kaisha Kobe Seiko Sho Dispositif de reforming d'hydrocarbure
EP0435642A2 (fr) * 1989-12-26 1991-07-03 The Tokyo Electric Power Company Incorporated Appareil pour la reformation d'hydrocarbures
WO1998052868A1 (fr) * 1997-05-23 1998-11-26 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. Dispositif pour le reformage d'eduits contenant des hydrocarbures

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DK165946C (da) * 1985-03-21 1993-07-05 Haldor Topsoe As Reformingproces under varmeudveksling og reaktor dertil
DE3532413A1 (de) * 1985-09-11 1987-03-12 Uhde Gmbh Vorrichtung zur erzeugung von synthesegas
JPH0642940B2 (ja) * 1987-03-31 1994-06-08 東洋エンジニアリング株式会社 気体吸熱反応用装置
DE3806408A1 (de) * 1988-02-29 1989-09-07 Uhde Gmbh Verfahren und vorrichtung zur erzeugung eines h(pfeil abwaerts)2(pfeil abwaerts) und co-enthaltenden synthesegases
EP1100616A4 (fr) * 1998-07-09 2002-02-06 Washington Group Int Reacteur centrifuge
WO2000063114A1 (fr) * 1999-04-20 2000-10-26 Tokyo Gas Co., Ltd. Reformeur cylindrique monotube et procede pour faire fonctionner ledit reformeur

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1988001983A2 (fr) * 1986-09-15 1988-03-24 L. & C. Steinmüller Gmbh Reformeur pour le craquage catalytique d'hydrocarbures gazeux
EP0360505A2 (fr) * 1988-09-19 1990-03-28 Kabushiki Kaisha Kobe Seiko Sho Dispositif de reforming d'hydrocarbure
EP0435642A2 (fr) * 1989-12-26 1991-07-03 The Tokyo Electric Power Company Incorporated Appareil pour la reformation d'hydrocarbures
WO1998052868A1 (fr) * 1997-05-23 1998-11-26 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. Dispositif pour le reformage d'eduits contenant des hydrocarbures

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006045746A1 (fr) * 2004-10-20 2006-05-04 Shell Internationale Research Maatschappij B.V. Procede de preparation d'un melange de monoxyde de carbone et d'hydrogene
WO2006045744A1 (fr) * 2004-10-20 2006-05-04 Shell Internationale Research Maatschappij B.V. Procede pour le reformage de vapeur et/ou de co2 d'une matiere premiere hydrocarbonee
EP2495214A3 (fr) * 2011-03-04 2013-01-23 DBI- Gastechnologisches Institut gGmbH Freiberg Procédé et dispositif pour reformage vapeur de gaz contenant des hydrocarbures
CN105189345A (zh) * 2013-03-25 2015-12-23 住友精密工业株式会社 燃料改性器及燃料电池
EP2955153A4 (fr) * 2013-03-25 2016-03-09 Sumitomo Prec Products Company Ltd Reformeur de combustible et pile à combustible
CN105189345B (zh) * 2013-03-25 2016-11-30 住友精密工业株式会社 燃料改性器及燃料电池
JPWO2014156013A1 (ja) * 2013-03-25 2017-02-16 住友精密工業株式会社 燃料改質器及び燃料電池
US9738519B2 (en) 2013-03-25 2017-08-22 Sumitomo Precision Products Co., Ltd. Fuel reformer and fuel cell
WO2020035706A1 (fr) * 2018-08-17 2020-02-20 Geoffrey Gerald Weedon Reformage à la vapeur ou à sec d'hydrocarbures
JP2022506005A (ja) * 2018-08-17 2022-01-17 テクニッシュ （トリニダード） リミテッド 炭化水素の水蒸気改質又は乾式改質

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